Process Flowstream  Collection System

ABSTRACT

A device and process for separating liquid and gas phases in a flowstream containing a liquefied gas or supercritical fluid under pressure mixed with a liquid. A splitter vessel separates the liquid from gas phases and transfers liquid to a collection container while conducting the gas phase out of the splitter. Separation of liquid phase out of the flowstream is provided without additional pressure schemes or solvent extractions imposed on the stream.

FIELD OF THE INVENTION

The present invention relates to sampling and collecting from a processflowstream containing a liquefied gas or supercritical fluid underpressure mixed with a liquid.

BACKGROUND OF THE INVENTION

In general, many process systems contain a mobile flowstream containinga liquefied gas or supercritical fluid under pressure mixed with aliquid. Any dissolved liquid samples or components of interest carriedthrough the process system will also remain dissolved in the flowstream.The principle that simple decompression of the mobile phase flowstreamseparates the stream into two fractions has great importance with regardto recovering liquid phase out of the flowstream. Removal of the gaseousphase, which can constitutes 50% to 95% of the flowstream during normaloperation is critical to successful and efficient recovery of the liquidphase.

In prior collection systems for supercritical chromatography systems,the separation of liquid and gas phases within the process flowstream isenhanced by expanding the flow path prior to entering a collectioncontainer, thus eliminating the need to pressurize the collectioncontainer. Typically, when the gaseous phase of the flowstream exits ata cold temperature from a flow tube in a room-temperature collectioncontainer causing the gas to heat up. When a collection container isfilling with liquid phase, the heating and expansion of the coldergaseous phase can cause an effervescence of bubbles at the surface ofthe liquid in the container, especially when the liquid level approachesto the inlet flow stream discharge. Further, this effect is not limitedto only supercritical process flow systems. Any type of process that isdesigned to recover liquid portions from a high pressure flowstreamcontaining a liquefied gas or supercritical fluid under pressure mixedwith a liquid can experience this problem. The effervescence effect cancause an aerosol to form and result in a slight loss of liquid. Eventhough the loss of liquid is minimal when compared to a much largervolume of liquid collected from the flow stream, some solids dissolvedin the liquid phase are potentially carried out of the collection devicevia the aerosol into a waste gas phase stream. The solids canprecipitate from the aerosol and cause build-up and blockages in theoutlet line leading from a collection device or a buildup of solids onliquid level sensors in the collection device.

Further, as the collection device fills with liquid, the expandinggaseous phase in the device creates some pressurization of the devicebefore it escapes in an outlet line, for example five to fifteen PSI,even if the pressurization is not necessary for gas/liquid separation.Other parts of the waste flow stream may induce higher backpressure thanis necessary for gas/liquid separation. Many collection devices are notmanufactured to withstand even moderate pressurization. Thus, for manylarge size (one liter or more) collection bottles, even moderate amountsof pressure could cause breakage that would spill valuable liquidsamples collected from the system.

SUMMARY OF THE INVENTION

The device and process of the preferred and alternative embodimentsefficiently separate liquid and gas phases from a flowstream containinga gas or supercritical fluid under pressure mixed with a liquid andcollects the liquid fraction at or near atmospheric pressure in acollection splitter device that is separate from a collection container.Separation of liquid samples out of the flowstream is provided withoutadditional pressure schemes or solvent extractions imposed on the flowstream samples.

Aerosol formation of the liquid phase is a common problem in samplecollection from a flowstream containing a liquefied gas or supercriticalfluid under pressure and mixed with a liquid. This is a significantcause of loss of the liquid phase that contains dissolved, and usuallyvaluable, solute(s) of interest. Higher temperatures may reduce theaerosol generation, and the composition of the separated phases also isa factor.

To collect liquid samples out of the high pressure flowstream, adecompression point for the flowstream is located prior to, andseparated from, the collection vessel. Initial separation of the liquidphase sample from gas phase occurs immediately at the point of initialdecompression. By providing an upstream restriction from the point ofdecompression, such as a backpressure regulator, a minimum backpressuresufficient to prevent an explosive expansion of gas from the flowstream,prevent precipitation of solids, and/or freezing of transfer lines canbe maintained in the collection system and transfer lines.

The preferred embodiment of the collection splitter device provides forrapid separation of volumes of the sample fractions from the highpressure flowstreams described above. Zones of restricted orunrestricted separation and flow within the splitter provide forseparation of the mixed flowstream. The result directs separated gas upand out of the splitter container while preventing gas from followingthe separated liquid down via gravity to a collection container locatedaway from the splitter. The aerosolization effect at the surface of avolume of collected liquid phase in the high-pressure system is avoidedby moving the gas/liquid separation process away from the liquid volumecollection device. In the present invention, this means that thesplitter device is a chamber that is separate and distinct from thepoint of liquid phase sample accumulation.

BRIEF DESCRIPTION OF THE DRAWINGS

For a better understanding of the nature of the present invention, itsfeatures and advantages, the subsequent detailed description ispresented in connection with accompanying drawings in which:

FIG. 1 illustrates a detailed view of the preferred collection splitter;

FIG. 2 illustrates flow of mobile phases through the preferredcollection splitter;

FIGS. 3( a) to 3(c) illustrate alternative embodiments of the collectionsplitter

FIG. 4 illustrates the preferred embodiment in a support frame;

FIG. 5 illustrates a cross-section of a support frame;

FIG. 6 illustrates the preferred collection splitter with liquid levelsensors; and

FIG. 7 is a flowchart of a method of the preferred embodiment;

FIG. 8 is a flowchart of a method of the preferred embodiment;

FIG. 9 illustrates an exemplary supercritical fluid chromatographysystem that can implement the collection splitter of the preferredembodiment.

DETAILED DESCRIPTION OF THE INVENTION

The preferred embodiment is used in the collection process of liquidphase samples or flow from a flowstream. The liquids can be from all orpart of a process flow system containing a liquefied gas orsupercritical fluid under pressure mixed with a liquid and collects theliquid phase separated from the flowstream at or near atmosphericpressure. The preferred embodiment can be use for reaction monitoring,process control, preparative chromatography and extraction usingsupercritical and near critical materials.

Referring to FIG. 1 and the exemplary method shown in FIG. 2, aflowstream is created in the system 10 whereby a sample can be injectedS80 via injection valve 30 into chromatography column 28, where thesample components of interest are separated S81. To begin a gentle,physical separation of the gas phase from the liquid phase in theflowstream S82, it is usually beneficial to slow the velocity of fluidswithin the transfer tubing 42. The fluid velocity is slowed inside thetransfer tubing by 42 placing a restrictive orifice or an equivalentrestrictions such as a smaller diameter tube or valve immediatelydownstream from first heater in the series if heater are implemented ina system. The high-pressure, high velocity flowstream exits heater 36and enters a restrictive orifice implemented as a flow restrictor 38,which provides a higher backpressure through heater 36 and thereby slowsthe flowstream and increases the contact time of the of liquid phase tothe heater 36. The restrictor 38 also insures a high enough backpressureto prevent freezing of liquid in the flowstream or precipitation ofsolutes out of the flowstream. The restriction increases thebackpressure in the heated zone and reduces the amount of gas expansion.

In the exemplary system of the mixed flowstream, it is also necessary toapply thermal conditioning of the flowstream to prevent uncontrolledcooling of fluids within the transfer lines due to rapid expansion ofthe gas phase during gas/liquid separation processes that occur withinthe transfer lines. Without thermal control, freezing of the flowstreamwithin the lines and connections will occur, causing clogging and systemshutdown. To gently heat the transfer tubing in the areas whereseparation processes begin to occur, passes tubing 42 passes through thetrim heaters 36 and 40. Alternatively, the entire separation componentsthat further include valve 43, splitter 46, and attached transfer linescould be heated to counter any uncontrolled cooling that occurs. In analternative exemplary embodiment, the velocity of fluids can be slowedafter all heaters, however, such a configuration may not control thefinal expansion of gas phase. As a result, the ability to activelysuppress aerosol formation within the transfer lines and within thecollection system may be diminished. After exiting the trim heater 40,flow is directed into the collection system. Alternative systems coulddirect portions of the flowstream to different collection systems, asinlets to different processes, or to a waste stream. Sensors andcontrollable components of system 10 are connected to a controller 11that receives data from and controls the pumps, 18 and 21, detector 32,heaters 36 and 40, valve 43, and collection container 48.

The preferred embodiment can passively separate liquid phase flow fromthe gas phase at or near atmospheric pressure, without applying apressure scheme to the separation or the collection vessel. Instead ofexpanding and separating the mobile phase flow in a collection deviceunder a pressure force, a vessel is provided in the flowstream prior toflow entering a collection vessel. In FIG. 1 and in the more detailedillustration in FIG. 2, the preferred embodiment of the collectionvessel is illustrated as a gas and liquid phase separation splitter 48that is set apart from the end-point liquid phase collection container50. Splitter 48 receives the mobile flow stream from transfer tube 58that is connected to valve 43. Splitter 48 can receive either continuousflow or an intermittent, pulsed flowstream. Splitter 48 depressurizesthe mobile flowstream and allows gasses to expand out of the flowstreamfor conducting to a waste gas line 60 using venting, pumping, or vacuumprocesses. By allowing the flowstream to gently expand in the hollowchamber of splitter 48, gasses are separated S84 from the liquids withminimal or no creation of aerosols.

Exposing the flowstream to a larger-diameter splitter 48 slows thestream's linear velocity, allowing gas to expand and separate from theflowstream. Slowing the linear velocity reduces the magnitude of shearforces occurring between mobile stream gasses and the liquid flow streamin transfer lines leading to a collection vessel. By lowering shearforces in the flow stream, there is less tendency for the stripping ofliquid phase into separated gasses, thereby creating an aerosol.Stripping forces cause aerosols, containing liquid samples, to escapecollection and proceed into the waste discharge, thereby losing valuablevolumes of samples.

When a flowstream volume enters the splitter, the hollow internal volumeof splitter 48 causes the gasses in the biphasic flowstream to expandand separate from the liquids. Liquid drains along walls of splitter 48,through transfer tube 58 to collection vessel 50 and gasses that havebeen substantially separated from the liquids leave the splitter. As aresult, the flow stream does not re-aerosolize or disturb liquid beingcollected in a collection vessel 50. Although some minimal pressureexists inside splitter 48 during a process run due to backpressure fromthe gas stream, no pressure scheme is applied in the splitter 48 orcollection vessel 50.

Referring to FIG. 3, when discharging the mobile phase flow stream inthe splitter 48 chamber, the flowstream should discharge against theinner wall of the splitter on a downward angle from horizontal on thedown-sloping part of the splitter wall. If the flowstream strikes thewall of the splitter at a horizontal angle or upward angle abovehorizontal, an undesirable effect of the upward force causes the liquidto aerosolize or to remain combined with the gas and can be lost throughwaste stream 60. The delivery tube 59 is brought arbitrarily close tothe wall of splitter 48 but does not need to be positioned against orparallel to the inner splitter wall since the separation of theflowstream does not use a cyclonic separation technique. However,discharging the flowstream against the wall of the splitter from adelivery tube placed close to the wall reduces the potential for aerosolformation. When the flowstream contacts the splitter wall, the flowstream spreads over a much larger surface area in which to escape at ornear atmospheric pressure, and it allows the gas in the thinnedflowstream a greater surface area to escape from the liquid. Thepressures within the splitter in operation of the preferred embodimentrange at less than 5 p.s.i. The liquid phase may swirl around thesplitter prior to draining down into the collection container 50, butthis effect is not necessary for separation and collection of the liquidphase stream. It is undesirable to direct the discharge tube 59 becomesangled straight down towards drain tube 52, since this would cause aturbulent discharge of the flowstream resulting in aerosol formation.

The splitter 48 is preferably formed cylindrically with tapered, openends that are smaller in diameter than the chamber of the splitter. Asdescribed more fully below, alternative shapes of splitter 48 may varyby size and shape yet still fall within the scope of the claimedinvention. The length of either the tapered, bottom-end 47 of thesplitter 48 and/or a drain tube 52 should be sufficiently long so thatthe liquid phase samples separated from the gasses in the flowstream aresufficiently unaffected by the gasses escaping out of the splitter 48.This length 47 will vary depending upon the flow rate of the processsystem 10, the volume of samples being collected, and the chemical andphysical compositions of the flowstream.

The sample collection container 50 is connected to splitter 48 viatransfer tube 52 to catch liquid phase that gravity-drains S86 intoliquid phase collection container 50. Drain tube 52 is connected tosplitter 48 with a pressure-resistant and leak-proof connector 54 and isconnected to collection container 50 with an equivalent connector 56.Splitter 48 is connected to a gas phase vent line 60 near the top-end ofsplitter 48 (the bottom-end of splitter 48 being the end connected togravity drain tube 52). Gasses emanating from the phase-separated mobileflow stream are conducted out of splitter 48 by venting or removalthrough transfer tube 60 to waste line 46.

Although the splitter has no pressure applied from devices in thecollection system, the splitter becomes mildly pressurized duringseparation processes because of the discharge of the gas phase in thesplitter 48 and restrictions to the collection vessel 50 and waste line46. The pressurization is useful for safety and waste flow purposes toensure elimination of gasses out of the splitter 48. For example, oneimplementation of the splitter 48 resulted in pressures ranging fromatmospheric up to 5 p.s.i. within the splitter 48 during operation.However, the splitter can operate with internal pressures at 100 p.s.i.or less provided that the splitter materials of manufacture are properlyspecified to handle higher pressures. A pressure gauge and sensor 62 maybe installed at the splitter to monitor pressure inside splitter 48.

Removing the liquid sample collection from a gas/liquid separationfunction provides important advantages of using nearly any volume ofliquid phase to be collected in any size of collection container 50desired. Most separated gasses are prevented from entering thecollection container 50 due to the restriction between the splitter andcollector. This also allows even small amounts of liquid recovery. Thepreferred embodiment creates zones within the splitter to provide forseparation of the mixed flowstream. The result directs separated gas upand out of the splitter container while directing separated liquid downvia gravity to a separate collection container. The increased diameterof the body of the splitter provides a zone within the wider diameterbody for gas to separate, rise, and exit the splitter unrestricted. Thereduced diameter at the splitter bottom creates a restricted zone forthe gas that disrupts any of the separated gas from traveling down thebottom of the splitter, though a connection tube, and into thecollection container. However, the restricted zone must also provideunrestricted flow of the separated liquid phase out of the bottom of thesplitter and into the collection container. As described herein, thepreferred splitter will vary in diameter and volumetric capacityaccording to the flowrate, liquid/gas mixture percentage and compositionof the flowstream, and pressure of the flowstream in the laboratory orindustrial scale system. However, regardless of the size of the splitterapplied to a particular flowstream, the two zones of unrestricted gasseparation and gas restriction/unrestricted liquid flow must bemaintained to cause the desired effects of passive liquid collection toa collection container located away from the separation zones. Eventhough gasses are restricted from the collection vessel 50, someseparated gasses from splitter 48 will still enter container 50, butbecause of the narrow, restricted drain tube 52 the vast majority of gasexits splitter 48 through waste line 60.

Since the splitter chamber 48 performs the function of “splitting” theprocess flowstream into separate gas and liquid flowstreams, an aspectof the various possible design proportions maintains the bottom-end ofthe splitter and the drain tube at a narrow enough diameter to minimizethe gas from the flowstream from entering into the collection container50. Gas re-contacting the liquid phase could cause re-aerosolization ofliquid samples that have already been separated and collected intocontainer 50. The diameter and length of tube 52 should be specifiedaccording to the volumetric flow, velocity, and composition of gasversus liquid in the process flowstream. The tube 52 should berestrictive to gasses so as to disallow gasses within the splitter 48from freely passing through tube 52 and entering a collection device.Another aspect of splitter 48 is that the diameter of the bottom-end ofsplitter 48 and the diameter of drain tube 52 are not so restrictive asto prevent liquid phase from draining into container 50 without backingup into splitter 48 and will also not prevent any quiescent gasses fromrising up out of container 50 and entering into splitter 48 toeventually discharge as waste.

These design considerations take into account that if effervescence ofliquid does occur in collection container 50 due to gas entering thecontainer 50, the possibility of re-aerosolization of liquids that couldbe swept back into splitter 48 is significantly reduced. Thisconfiguration provides for scalable collection of liquid samples forexample from fifty milliliters up to twenty liters or more simply bychanging the scale and geometry of the collection system 44.

FIGS. 4 a-4 c illustrate alternative embodiments of splitter 48. Thepreferred embodiment of splitter 48 is illustrated in FIGS. 1 and 2 asgenerally perpendicular teardrop design that provides adequate expansionand separation of the flowstream and a smooth transition of the innerwalls for gravity draining of liquid phase samples to the bottom of eachsplitter. FIG. 4 a shows an alternative splitter 64 comprising a largerdiameter of internal separation space. FIG. 4 b shows an alternativesplitter 66 having a more straight-walled separation space but stillretaining smoothed transitions in the walls that lead down to a lowerend for gravity draining of liquids. FIG. 4 c shows yet anotheralternative embodiment of a splitter 68 that has a curved walled designthat is more uniform in shape than splitter 48 and narrower in shapethan alternative splitter 64.

The shape of splitter 48 is preferably formed with a smooth inner wallthat gradually decreases in internal cross-sectional area or diameter,which allows the liquid phase separating out of the flowstream totraverse down the inner wall under gravity flow and collect at thebottom of the device without forming droplets on ridges, bumps, ortransitions in the inner wall. The discharge tube carrying the initialflowstream into splitter 48 is preferably directed at an angle less thanhorizontal inside the splitter to discharge liquid samples downward fromhorizontal towards the down-sloping section of the splitter wall. Thisdesign provides the advantages of collecting liquid samples to container50 while preventing spraying the incoming flowstream upwards causingaerosolization and loss of sample. As one skilled in the art willobserve, the sizes and volumes of collection system 44 of the preferredembodiment are exemplary.

The splitter wall is preferably formed with a decreasing diametertowards the bottom end and is not entirely perpendicular to horizontal.Although it would still function as a splitter and is included in thescope of alternative embodiments, a perpendicular inner walled vesselsuch as a true cylindrical or rectangular shape with flat ends couldcause the undesirable effects of deflection of liquid phase fractionssubstantially upward inside the splitter resulting in furtheraerosolization (and loss of liquid through the vent line 60) and/orcause pooling of liquid on a flat bottom of such a design. As a furtherexample, an alternative of the splitter 48 could be constructed as athree-dimensional diamond shape, but such a formation would not functionas efficiently as those shown in FIGS. 4 a-4 d. One skilled in the artwill understand that exact sizes, shapes, flow stream capability, andmaterials of construction of the splitter may vary depending on linearvelocity, volumetric flow rate, configuration and size of the systemassembly, composition of the flowstream, and other factors incorporatedinto a process design and operation. For example, an industrialimplementation would scale the splitter and collection container designand construction materials for high capacity and strength.

The splitter 48 should be constructed with inert glass, plastic,composite, or metal materials appropriate for and compatible withsamples and compounds being collected from the flowstream. Although notnecessary for the present invention, for safety purposes, any deviceused as a gas/liquid splitter should have adequate strength to withstandpotentially dangerous pressure fluctuations associated with the upstreamprocess being operated. For example, glass splitters may be treated witha shatter-resistant coating.

In FIG. 1, collection container 50 is the final liquid stream collectionpoint in the system 10. However, the separated liquid phase could bedirected to any collection unit desirable or fed as an inlet flowstreamto an additional process. Container 50 may be constructed of glass,plastic, or metal capable of handling the liquid under collection, andthe preferred embodiment used plastic-coated glass as a safety factoragainst possible breakage due to an improper overpressurization of thecollection system.

During separation of the flowstream, some gas may enter the collectioncontainer 50 along with liquid flow. This de minimis gas flow can beintegrated into an automation of collection system 44. To prevent leaksout of the container 50, cap 56 should be sealed with an appropriateseal such as an O-ring. FIG. 5 shows a detailed view of collectioncontainer 50 with a dip tube 53 and various liquid level sensors tomonitor liquid levels S88 in container 50. Dip tube 53 passes throughcap 56 into container 50. As the liquid 69 of liquid phase fractionsrises in container 50, the reservoir air space, which may contain somegas entering from splitter 48, compresses slightly. The dip tube 53 ispreferably a clear plastic tube that has a first capacitance sensor 70and a second capacitance sensor 72 attached to the tube 53. The sensorsare calibrated to require a greater thickness of liquid in the dip tube53 than merely a liquid film draining through tube 53. The dip tube 53is positioned to reach into collection container 50 such that when theliquid level 68 reaches the bottom of the dip tube 53, the reserve airhas no place to vent and (previously up through tube into splitter 48and waste tube 50) the container reaches a point that the liquid phasedraining into container 48 begins filling dip tube up until it fillspast first sensor 70.

Sensors in system 10 can be connected to controller 11 that determinescollection container 50 is nearly full, and the controller triggers anaction to prevent overfilling of container 50. One action is to signalprocesses feeding the flowstream into the process system to stopproduction and introduction of the flowstream into the system 10. Thisaction allows flowstream already sent to the collection system tocomplete separation in splitter 48. After stopping the flow intocollection system 40, a final volume of the flowstream has passedthrough the collection system 10, the liquid phase is drained fromsplitter 48 into the backed-up dip tube 53. By maintaining extraairspace space within container 50, when cap 56 is opened to theatmosphere, air from container 50 escapes allowing pressure to normalizeand the liquid phase in dip tube 53, that siphoned up the tube, can nowgravity drain back into the collection container 50 without overfilling.

An additional second sensor 72 could also be placed higher above firstsensor 70 on dip tube 53. Second sensor 72 triggers a complete system 10shut-down that prevents any further flowstream from entering splitter48. Even after the first sensor 70 prevents further flow into collectionsystem 40, the system 10 may contain a greater volume of liquid that thecollection container 50 can hold. The second sensor 72 notifies thesystem 10 that the liquid level currently in the tube 53 will completelyfill collection container 50 and therefore a complete and immediatesystem shut-down is necessary to prevent overfilling of the collectioncontainer 50.

Since physical separation of the flowstream is performed upstream of theliquid fraction collection container 50 in splitter 48, any number ofcollection containers can be implemented with the preferred embodimenthaving appropriate valving and tubing between each container and thesystem 10. FIG. 6 illustrates two discrete, upright collection splitters48 and 49 preferably attached to a common manifold support structure 74.Splitter 48 receives a flowstream from line 58 and splitter 49 receivesa flowstream from line 61. Liquid phase from splitter 48 drains throughline 52 into collection container 50, and liquid phase from splitter 49drains through line 55 into collection container 51. A cross-sectionA-A′ of manifold support 74 is also illustrated in FIG. 7. Splitters 48and 49 are attached to manifold 74 using appropriate airtight andpressure-tight connectors. A connector 79 connects to the top of asplitter device and creates an airtight and pressure-tight seal withmanifold 74. Gas phase from both splitters 48 and 49 enter channel 76which transfers to a waste system. Here, and in all configurations ofthe preferred and alternative embodiments, chemically sensitive sealsfor connections should be avoided. Seals that react with chemicals inthe system can swell in-place and either restrict system flow and causebackpressure or fail and allow fluids to escape.

Although two collection systems 44 are shown in FIG. 6, an alternativeembodiment of more than two devices could be used in a process byduplicating the configuration of devices and associated equipment shown.Separation of gasses from the mobile phase occurs quickly and simply insplitters 48 and 49, upstream of the collection containers 50 and 51.Thus, the large volumetric capacity of liquid phase retention in thepresent invention removes time-consuming bottlenecks caused byadditional processes typically found in SFC sample solute collectionprocesses and promotes rapid sample injection, elution, and collection.

Referring specifically to FIG. 7, manifold support 74 includes at leastone hollow channel 78 (only one channel 78 is shown for illustrativepurposes). Channel 78 receives mobile phase flow from tubing 58 andconducts the mobile phase flow stream into a splitter 48. Additioncomponents connected to splitter 48 through manifold 74 may include apressure sensor and gauge to measure pressure inside the splitter 48during separation processes. The manifold 74 also provides a pathway outof splitters 48, 49 for waste gasses. Internal to manifold 74 is acommon hollow channel 76 that communicates with each splitter where eachsplitter connects to the manifold 74 in connection 79. Channel 76receives the gasses and vapors inside of each splitter that separate outof the mobile phase flow stream. The gasses are vented to an appropriatewaste system.

The alternative embodiment has an advantage of allowing unattendedprocess runs that can be combined with a rapid flowstream productionprocess to provide a high volume of collection capacity without renewingthe collection system. Unattended process runs may require monitoringfill levels in each collection container according to the descriptionrelating to FIG. 4. Instead of a shut-down of flowstream production bysensor 70 or system shutdown by sensor 72, when liquid reaches athreshold level sensor 70 in container 50, a valve could re-direct theflowstream to splitter 49 and container 51 without stopping theflowstream. A conventional method for monitoring fill levels would be tovisually observe the height of liquid in each collection container.

FIG. 9 illustrates a flow diagram of an alternative embodiment of thepresent invention comprising a process stream fed from a supercriticalfluid chromatography (SFC) or supercritical fluid extraction (SFE)system. For the purposes of the alternative embodiment, an SFC system isdescribed. In general, dissolved samples carried through an SFC systemalso remain dissolved in the liquid organic modifier phase. Theprinciple that simple decompression of the mobile phase in SFC separatesthe stream into two fractions has great importance with regard to usethe technique in a preparative manner. Removal of a gaseous carbondioxide (CO2) phase, which constitutes 50% to 95% of the mobile phaseduring normal operation, greatly reduces the liquid collection volumefor each component and thereby reduces the post-chromatograhicprocessing necessary for recovery of separated components. Expanding thetechnique of analytical SFC to allow preparative SFC requires severaladaptations to the instrument. First the system requires increased flowcapacity. Flows ranging from 10 ml/min to 200 ml/min are suitable forseparation of multi-milligram up to gram quantities of materials.

In FIG. 9, SFC system 90 has a first flow stream 92 of a highlycompressed gas, compressible liquid, or supercritical fluid. Althoughmany compounds, liquid or gas, could be used in the first flow stream,the preferred embodiment supplies the first flow stream with liquefiedcarbon dioxide (CO2) gas contained in cylinder 94. High pressuretransfer tubing connects CO2 source 94 to pump 98. Gas from tank 94 maybe cooled through line chiller 16 prior to being compressed in pump 18.Downstream flow from pump 18 may have a dampener and pressure transducer104 prior to mixing with a second flow stream 100. The second flowstream 20 is supplied from a relatively incompressible liquid, which inthe preferred embodiment is a compound such as methanol that is suppliedfrom modifier supply tank 102. The system uses two SFC-grade or modifiedreciprocating pumps that can supply adequate pressures and flow ratesfor the system 90. Pump 101 supplies modifier flow from tank 102 underpressure to mix with flow stream 92. Flow streams 92 and 100 combine andenter a mixing column 26, creating a mixture of modifier solventdissolved into the supercritical fluid. The combined stream is pumped bypumps 98 and 101 at a controlled mass-flow rate and enters packedchromatography column 108.

The SFC system in the alternative embodiment can provide for flows ofapproximately 20 to 100 ml/min total flow (CO2 plus modifier flow) inthe highly compressed state from the pumping system. However, flowratesfor alternative embodiments and SFC systems could range up to orders ofmagnitude higher or lower through adjustment or substitution of systemhardware and flow parameters. Packed column 108 receives sampleinjection at its head from injector 110, where a sample of interest isinjected into the flow system. Once a bi-phasic, mobile phase flowstreamexits a column, expanding gas, such as CO2, causes a severe temperaturedrop that has the possibility of forming dry ice and clogging thesystem. Since flows of preparative SFC systems are much higher thancorresponding analytical systems, considerably more heat must be addedto compensate for the temperature drop. Care must be taken, however, notto allow the actual temperature to rise in the flow system since thismay cause damage to thermally unstable compounds of interest. Higherorganic modifier content reduces the severity of this problem, both byadding heat capacity and by dissolving the CO2, thereby preventing dryice formation.

After fractionation of the sample occurs in the column 108, the elutionmixture passes from the column outlet into a detector 112 and thenenters backpressure regulator 114 (BPR). Expanded elution fluid exitsthe BPR 114 at a velocity of approximately two to five times the flowvelocity upstream of BPR 34 and under pressure of approximately twentyto forty bars. Variations in the expansion occur as a result of thechanging modifier solvent concentration from 2.5 to 50 percent over thecourse of a separation.

Initial separation of the liquid phased sample from CO2 gas occursimmediately at the point of initial decompression within the BPR 114. Byproviding downstream restriction, a minimum backpressure sufficient toprevent the formation of solid CO2 can be maintained while liquid CO2 ispresent in the thermally-regulated transfer lines 122. The degree of CO2evaporation is a function of both the available heat transfer in thisregion and the downstream flow restriction which limits the amount ofexpansion available to the decompressing fluid. Due to the pressure dropacross the BPR 114, a fraction of the emerging CO2 will evaporate,typically causing a significant drop in the temperature of the emergingfluid.

Due to the expansion, linear velocities of the depressurizing fluidincrease dramatically in the transfer tubing. Residual liquids of thesystem are moved along the flow path largely by shear forces from theexpanding gas. This turbulent environment is ideal for the creation ofaerosols, whereby very small droplets of modifier liquid are entrainedin the gas phase as a “mist.” It is a finding of this study that theaerosol formation within the transfer tubing can be almost completelycontrolled by proper temperature control of the expanding two-phasesystem. Aerosol formation is a greater problem at lower temperatures. Itis a surprising finding of this work that higher levels of organicmodifier with correspondingly lower CO2 content require highertemperature levels to prevent visible aerosol formation.

From BPR 34, the flowstream passes one or more heaters, that may bemounted in series, to heat the elution fluid. In FIG. 9, evaporatorheater 116 and a trim heater 120 are mounted in series after the BPR114. The evaporator heater 116 is heated with an appropriately sizedcartridge heater and controlled by an appropriate heater controller.Transfer tubing 122 is tightly coiled around the heating assembly andoptimized for thermal contact. The elution fluid is heated to within thecontrol temperature of the evaporator 114, which is betweenapproximately 5 to 50 degrees C., to protect heat sensitive compoundsfrom being damaged. The objective is to boil CO2 out of the elutionfluid as the fluid passes through the evaporator 116. To complete therequired heat transfer, biphasic elution fluid inside transfer tubing122 enters the final heat exchanger, which is a trim heater 120. In thepreferred embodiment, the trim heater setting is typically above theevaporator setpoint. Heater 120 is used not only to suppress aerosolformation within the transfer tube 122 but also to control the level ofdissolved CO2 in the liquid phase.

During the CO2 evaporation process within the first heated zone,significant separation between the gaseous CO2 and liquid modifieroccurs. However, the separation to pure CO2 and pure organic modifier isnever realized. Some organic modifier is typically evaporated into thegas state. The degree of evaporation is largely dependent on theabsolute temperature of the fluids within the transfer tubing 122. Whileorganic modifier evaporation does lead to lower recovery of liquid phasewhen it reaches a collector, it does not necessarily reduce the recoveryof dissolved components of interest which do not typically have lowenough boiling points to convert to vapor. A fraction of CO2 will alsoremain dissolved in the organic liquid modifier. Both temperature andpressure determine the amount of residual CO2. Higher temperaturesreduce CO2 solubility while higher pressures increase CO2 solubility.Turbulent flow of the CO2 gas within the narrow tubing also produces astrong shearing force that propels the liquid down the walls of thetransfer tube 42. This very turbulent flow frequently causes smalldroplets at the liquid surface to rip away from the bulk liquid andbecome entrained into the rapidly moving gas phase of the fluid down thetransfer tube 122, which is called aerosol formation or “misting.”

After thermal conditioning, the flowstream is directed by valve 123 intosplitter 128. Separation of gasses from the mobile phase occurs insplitter 128 by creating the zones of restricted gas flow andunrestricted liquid flow, as described in the splitter 48 of thepreferred embodiment. Further, the features and design of splitter 128are also similar to those of the preferred splitter 48. Splitter 128 canperform separation of gas and liquid phases with either a continuous orpulsed flowstream. The creation of separation zones and the separationof gas and liquid phases are performed passively, where no pressurescheme is applied into splitter 128. Pressures within splitter 128 canrange from 100 psi or less, but are preferably 5 psi and less. Liquidseparated out of the flowstream has an unrestricted flow channel downinto a separate collection container 130, which is similar in design andfeatures of the collection container 50 for the preferred embodiment.Thus, the large volumetric capacity of liquid phase retention in thepresent invention removes time-consuming bottlenecks caused byadditional processes typically found in SFC sample solute collectionprocesses and promotes rapid sample injection, elution, and collection.

Sensors in system 90 can be connected to a controller 101 as shown inFIG. 9 similar to those described in the preferred embodiment.Controller 101 determines collection container 130 is nearly full, andthe controller triggers an action to prevent overfilling of container130. One action is to signal injector 110 to cease injection ofadditional samples. This action allows samples already in column 108 andmobile phase flow already in the system between column 108 and splitter128 to complete chromatographic fractionation and to complete separationin splitter 128.

One skilled in the art will appreciate that the present invention can bepracticed by other than the described embodiments, which are presentedfor purposes of illustration and not limitation, and the presentinvention is limited only by the claims that follow

1-9. (canceled)
 10. A process for collecting liquid flow from aflowstream containing liquefied gas or supercritical fluid underpressure mixed with a liquid, comprising receive the flowstream into asplitter; providing an unrestricted zone for gas phase in the flowstreamto separate from the flowstream and exit the splitter; providing arestricted zone that allows liquid phase to separate from the flowstreamand drain unrestricted out of the splitter and prevents the gas phasefrom following the path of the drained liquid phase out of the splitter.11. The process of claim 10, wherein the providing a restricted zonecomprises providing liquid phase drainage of the liquid phase out of thesplitter without applying a pressure scheme.
 12. The process of claim10, wherein the providing an unrestricted zone comprises venting of thegas flow out of the splitter without applying a pressure scheme.
 13. Theprocess of claim 10, wherein the splitter is formed with a smoothedinterior wall that reduces in diameter towards the outlet for liquidflow.
 14. The process of claim 10, wherein the outlet for liquid flow isformed on an elongated bottom end of the splitter that provides forgravity drainage of liquid flow out of the splitter.
 15. The process ofclaim 10, further comprising discharging the flowstream from a dischargeline that is extended into the splitter vessel through the inlet todischarge the flowstream at an angle less than horizontal and todischarge against an interior wall portion of the splitter that isformed at an angle towards the outlet for the liquid flow.
 16. Theprocess of claim 10, further comprising applying thermal conditioning tothe flowstream prior to the flowstream entering the splitter.